WO2009083227A2 - Procédé et dispositif pour séparer des constituants à point d'ébullition bas de mélanges d'hydrocarbures - Google Patents

Procédé et dispositif pour séparer des constituants à point d'ébullition bas de mélanges d'hydrocarbures Download PDF

Info

Publication number
WO2009083227A2
WO2009083227A2 PCT/EP2008/011049 EP2008011049W WO2009083227A2 WO 2009083227 A2 WO2009083227 A2 WO 2009083227A2 EP 2008011049 W EP2008011049 W EP 2008011049W WO 2009083227 A2 WO2009083227 A2 WO 2009083227A2
Authority
WO
WIPO (PCT)
Prior art keywords
condensation
boiling fraction
temperature level
mixture
distillation
Prior art date
Application number
PCT/EP2008/011049
Other languages
German (de)
English (en)
Other versions
WO2009083227A3 (fr
WO2009083227A9 (fr
Inventor
Johannes Menzel
Sascha Wenzel
Original Assignee
Uhde Gmbh
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority to BRPI0821955-9A priority Critical patent/BRPI0821955A2/pt
Priority to EA201070803A priority patent/EA201070803A1/ru
Priority to US12/735,255 priority patent/US20110041550A1/en
Priority to JP2010540068A priority patent/JP2011508031A/ja
Priority to CN2008801258704A priority patent/CN101932368A/zh
Priority to CA2710776A priority patent/CA2710776A1/fr
Application filed by Uhde Gmbh filed Critical Uhde Gmbh
Priority to MX2010007195A priority patent/MX2010007195A/es
Priority to EP08867264A priority patent/EP2225007A2/fr
Publication of WO2009083227A2 publication Critical patent/WO2009083227A2/fr
Publication of WO2009083227A3 publication Critical patent/WO2009083227A3/fr
Publication of WO2009083227A9 publication Critical patent/WO2009083227A9/fr
Priority to ZA2010/04516A priority patent/ZA201004516B/en

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/04—Purification; Separation; Use of additives by distillation
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/09—Purification; Separation; Use of additives by fractional condensation
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
    • F25J3/0219—Refinery gas, cracking gas, coke oven gas, gaseous mixtures containing aliphatic unsaturated CnHm or gaseous mixtures of undefined nature
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0238—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 2 carbon atoms or more
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0242—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 3 carbon atoms or more
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
    • F25J3/0252—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of hydrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/02—Processes or apparatus using separation by rectification in a single pressure main column system
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/74—Refluxing the column with at least a part of the partially condensed overhead gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/62—Ethane or ethylene
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/04—Internal refrigeration with work-producing gas expansion loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/12—External refrigeration with liquid vaporising loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/60—Closed external refrigeration cycle with single component refrigerant [SCR], e.g. C1-, C2- or C3-hydrocarbons
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/40—Vertical layout or arrangement of cold equipments within in the cold box, e.g. columns, condensers, heat exchangers etc.

Definitions

  • the invention relates to a method and apparatus for separating low-boiling components from a hydrocarbon stream, in particular for separating a C 2 fraction from a target desired C 3 + fraction, for example, in the dehydrogenation of light hydrocarbons, but also others Separation tasks in the C 1 to C 4 range.
  • distillation column is operated as a deethanizer and so designated, since all substances which have boiling points less than or equal to that of ethane in this deethanizer over Head to be separated.
  • the feed mixture Before entering the cold box, the feed mixture is first cooled to about -25 0 C. The resulting condensate is led directly into the deethanizer. The non-condensed vapors are further cooled within the cold box to about -90 0 C, wherein the resulting product-rich condensate is also passed to the deethanizer after heat exchange.
  • the coldbox thus represents a single-stage coarse separation.
  • the remaining vapor phase which contains substantially non-condensable components, for example hydrogen, is, after heat exchange in the stream entering the coldbox, relaxed. Due to the Joule-Thompson effect, the low boilers cool to about -110 0 C from. This temperature level is used to partially condense the stream entering the coldbox.
  • the uncondensed low-boiling components are essentially free of C3 + components.
  • the object of the invention is therefore to provide a method and a device are available in which the refrigeration consumption can be significantly reduced.
  • the invention solves this problem according to the main claim with a method for the separation of a starting mixture
  • a continuous distillation apparatus comprising at least one line for the supply of one or more starting mixtures, a lower boiling fraction discharge, a higher boiling fraction withdrawal and a heating device,
  • the distillation apparatus contains at least two condensation stages each having different temperature levels,
  • the respectively non-condensed subsets are each fed downstream separation internals or condensation stages, each with lower temperature levels and the respective condensed subsets via separating internals in the direction of the trigger for the higher-boiling
  • Condensation stage is returned to the lowest temperature level upstream section of the distillation apparatus,
  • the distillation apparatus contains three to five series-connected, each having different temperature levels having condensation stages.
  • the condensation stage with the lowest temperature level has a temperature of -120 0 C to -70 ° C at a pressure of at least 2 MPa absolute, preferably at least 3 MPa.
  • the mixture which leaves the distillation apparatus as a lower-boiling fraction, is relaxed, the mixture using the Joule-Thompson effect further cooled and thus to cool the condensation stage with the lowest Temperature level is used.
  • the relaxation is carried out with an expansion turbine.
  • the process is applied to starting mixtures which contain substantially hydrogen, hydrocarbons having up to two carbon atoms and hydrocarbons having at least three carbon atoms.
  • a mixture containing substantially hydrogen and hydrocarbons containing up to two carbon atoms is formed which contains substantially no hydrocarbons having at least three carbon atoms.
  • the deduction for the higher-boiling fraction falls a mixture containing at least three carbon atoms hydrocarbons, which contains substantially neither hydrogen nor up to two carbon atoms containing hydrocarbons.
  • the method is applied to starting mixtures, each containing less than 2 mol% of carbon dioxide and water or water vapor.
  • a reaction mixture of the catalytic dehydrogenation of hydrocarbons is used as starting mixture.
  • the segment of the distillation apparatus via which the condensed at the condensation stage with the highest temperature level subset of the starting mixture is supplied to the trigger for the higher-boiling fraction, as the stripping section of the distillation apparatus before.
  • starting mixtures are added with relatively low proportion of low boiling point components preferably below the condensation stage with the highest temperature level and starting mixtures with a relatively high proportion of low boiling point components preferably above the condensation stage with the highest Temperature level are added.
  • condensation stages are present as capacitors.
  • the condensation stages are cooled with cooling water, evaporating ammonia, propane, propene and / or by the utilization of the Joule-Thompson effect in the expansion of process gases.
  • the heating device is operated with external waste heat.
  • the invention also achieves this object with a suitable distillation apparatus for the separation of a starting mixture, comprising: • one or more lines for the supply of one or more
  • the distillation apparatus is in the form of a single distillation column or that the distillation apparatus is present as a cascade containing a plurality of distillation columns, wherein in each case capacitors are provided between the distillation columns.
  • capacitors By the use of the process according to the distillation device with several operating at different temperature levels capacitors is achieved that not the entire amount of cooling for the condensation at the lowest temperature level and thus must be provided with the highest cost. Instead, the intermediate capacitors operate at temperatures of about + 45 ° C, +15 0 C and -30 0 C, which is a further advantage of the invention.
  • FIG. 1 shows the process according to the invention, in which the distillation apparatus consists of a single distillation column with several intermediate condensers.
  • FIG. 2 shows the method according to the invention, in which the distillation device is constructed from a separate stripping part and reinforcing part.
  • FIG. 3 shows the method according to the invention, in which the distillation device is made up of three sections, the intermediate capacitors being located between the sections.
  • the vaporous feed mixture 1 for example, in an ammonia evaporator 2 are first cooled to 15 ° C.
  • a further heat exchanger 3 can be further cooled to about 10 0 C against the recovered C2 fraction 4, wherein a portion of the vapor condenses.
  • Vapor phase 5 and condensate 6 arrive separately in the distillation apparatus.
  • the task can also be carried out above the condensation stage with the highest temperature level.
  • the liquid in the distillation column 7 flows down and is partially re-evaporated.
  • the non-evaporated part is withdrawn as C3 + product 8 at the bottom of the distillation column 7.
  • the low boilers rise upwards as vapor and are partly condensed by the two-part first condenser 9, which is located above the feed tray, cooling water and ammonia being used successively as the coolant. Further rising vapors are partially liquefied in the second condenser 10, which is operated with the coolant propane or propene, so that only a small part of the vapors reaches the top condenser 11.
  • the vapors not condensed in the top condenser 11 form the C2 fractions 12 and 13, which is expanded following the condensation in the expander 14, wherein it cools to about -125 0 C.
  • This cooled vapor 15 is used as a cooling medium on the cold side of the top condenser 11, wherein it is heated to about -50 0 C.
  • this C2 fraction 4 passes through the heat exchanger 3 for cooling the feed mixture 1.
  • the liquid flows in the stripping section 16 down and is partially re-evaporated.
  • the unevaporated part is withdrawn as C3 + product 8 at the bottom of the stripping section 16.
  • the vaporous low boilers 17 flow into the two-part design, first condenser 9, where they are partially condensed, being used as a coolant sequentially cooling water and ammonia. Both the condensate 18 and the vapors 19 are added to the reinforcing member 20.
  • a portion of the sump of the reinforcing member 20 is used as a head template 21 of the output member 16.
  • the liquid in the stripping section 16 flows downwards and is partially re-evaporated.
  • the unevaporated part is withdrawn as C3 + product 8 at the bottom of the stripping section 16.
  • the vaporous low boilers 17 flow into the two-part design, first condenser 9, where they are partially condensed, being used as a coolant sequentially cooling water and ammonia. Both the condensate 18 and the vapors 19 are introduced into the first reinforcing member 22.
  • a part of the sump of the first reinforcement part 22 is used as a head template of the output part 16.
  • both the condensate and the vapors are added to a second enrichment part 23.
  • the sump of the second amplifying part 23 serves as a head template of the first amplifying part 22, in this way only a small part of the vapors reaches the top condenser 11.
  • the vapors not condensed in the top condenser 11 form the C2 fractions 12 and 13, which after the condensation is relaxed in the expander 14, wherein it cools to about -125 0 C.
  • This cooled vapor 15 is used as a cooling medium on the cold side of the top condenser 11, wherein it is heated to about -50 0 C. Subsequently, this C2 fraction 4 passes through the heat exchanger 3 for cooling the feed mixture 1.

Landscapes

  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Physics & Mathematics (AREA)
  • General Engineering & Computer Science (AREA)
  • Thermal Sciences (AREA)
  • Mechanical Engineering (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Water Supply & Treatment (AREA)
  • Analytical Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

L'invention concerne un procédé et un dispositif servant à séparer un mélange de départ en une fraction à point d'ébullition élevé et en une fraction à point d'ébullition bas dans un appareillage de distillation fonctionnant en continu qui comprend au moins une conduite pour l'amenée d'un ou de plusieurs mélanges de départ, une évacuation pour la fraction à point d'ébullition bas, une évacuation pour la fraction à point d'ébullition élevé, ainsi qu'un dispositif de chauffage. Selon l'invention, l'appareillage de distillation contient au moins deux étages de condensation ayant respectivement des niveaux de température différents, les étages de condensation respectivement en amont dans le sens d'écoulement des vapeurs présentant des niveaux de température respectivement supérieurs à ceux des étages de condensation respectivement en aval. Des garnissages séparateurs sont respectivement intercalés entre les étages de condensation. Des condensations partielles se produisent au niveau des étages de condensation, les quantités partielles respectivement non condensées étant respectivement amenées à des garnissages séparateurs ou à des étages de condensation en aval à niveaux de température respectivement inférieurs et les quantités partielles respectivement condensées étant dirigées par le biais de garnissages séparateurs vers l'évacuation pour la fraction à point d'ébullition élevé. Un milieu pratiquement gazeux est obtenu dans l'étage de condensation de plus bas niveau de température et y condense partiellement, la quantité partielle non condensée du milieu étant ramenée à l'évacuation pour la fraction de point d'ébullition bas et la quantité partielle condensée étant ramenée à une zone de l'appareillage de distillation située en amont de l'étage de condensation de plus bas niveau de température. L'étage de condensation de plus bas niveau de température présente une température inférieure à -40°C.
PCT/EP2008/011049 2007-12-28 2008-12-22 Procédé et dispositif pour séparer des constituants à point d'ébullition bas de mélanges d'hydrocarbures WO2009083227A2 (fr)

Priority Applications (9)

Application Number Priority Date Filing Date Title
EA201070803A EA201070803A1 (ru) 2007-12-28 2008-12-22 Способ и устройство для выделения низкокипящих компонентов из углеводородных смесей
US12/735,255 US20110041550A1 (en) 2007-12-28 2008-12-22 Process and apparatus for the separation of light-boiling components from hydrocarbon mixtures
JP2010540068A JP2011508031A (ja) 2007-12-28 2008-12-22 低沸点成分を炭化水素混合物から分離するための方法および装置
CN2008801258704A CN101932368A (zh) 2007-12-28 2008-12-22 用于从烃混合物中分离出易于沸腾的组分的方法和装置
CA2710776A CA2710776A1 (fr) 2007-12-28 2008-12-22 Procede et dispositif pour separer des constituants a point d'ebullition bas de melanges d'hydrocarbures
BRPI0821955-9A BRPI0821955A2 (pt) 2007-12-28 2008-12-22 Processo e dispositivo para a separação de componentes de baixa ebulição das misturas de hidrocarboneto
MX2010007195A MX2010007195A (es) 2007-12-28 2008-12-22 Metodo y dispositivo para separar componentes de bajo punto de ebullicion de mezclas de hidrocarburos.
EP08867264A EP2225007A2 (fr) 2007-12-28 2008-12-22 Procédé et dispositif pour séparer des constituants à point d'ébullition bas de mélanges d'hydrocarbures
ZA2010/04516A ZA201004516B (en) 2007-12-28 2010-06-25 Method and device for separating off low-boiling components from hydrocarbon mixtures

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102007063347A DE102007063347A1 (de) 2007-12-28 2007-12-28 Verfahren zur Abtrennung von leichtsiedenden Komponenten aus einem Kohlenwasserstoffstrom
DE102007063347.7 2007-12-28

Publications (3)

Publication Number Publication Date
WO2009083227A2 true WO2009083227A2 (fr) 2009-07-09
WO2009083227A3 WO2009083227A3 (fr) 2009-09-17
WO2009083227A9 WO2009083227A9 (fr) 2009-11-05

Family

ID=40690838

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP2008/011049 WO2009083227A2 (fr) 2007-12-28 2008-12-22 Procédé et dispositif pour séparer des constituants à point d'ébullition bas de mélanges d'hydrocarbures

Country Status (12)

Country Link
US (1) US20110041550A1 (fr)
EP (1) EP2225007A2 (fr)
JP (1) JP2011508031A (fr)
KR (1) KR20100125228A (fr)
CN (1) CN101932368A (fr)
BR (1) BRPI0821955A2 (fr)
CA (1) CA2710776A1 (fr)
DE (1) DE102007063347A1 (fr)
EA (1) EA201070803A1 (fr)
MX (1) MX2010007195A (fr)
WO (1) WO2009083227A2 (fr)
ZA (1) ZA201004516B (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2969746A1 (fr) * 2010-12-23 2012-06-29 Air Liquide Condensation d'un premier fluide a l'aide d'un deuxieme fluide

Families Citing this family (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US10852060B2 (en) * 2011-04-08 2020-12-01 Pilot Energy Solutions, Llc Single-unit gas separation process having expanded, post-separation vent stream
KR20180104620A (ko) * 2015-12-18 2018-09-21 벡텔 하이드로카본 테크놀로지 솔루션즈, 인코포레이티드 백-엔드 터보팽창기를 사용하여 정련 폐가스로부터 원하는 경질 탄화수소를 회수하기 위한 시스템 및 방법
WO2018037330A1 (fr) * 2016-08-25 2018-03-01 Sabic Global Technologies B.V. Procédé de séparation cryogénique pour effluent de réacteur de déshydrogénation de propane
CN109722267A (zh) * 2017-10-31 2019-05-07 珠海市启夏能源科技有限公司 一种塔罐组合式凝析油气化系统及其生产工艺
CN111545086B (zh) * 2020-05-27 2021-11-09 新疆大学 一种可逆开关型泡沫体系及其制备方法
FR3123971B1 (fr) * 2021-06-09 2023-04-28 Air Liquide Purification cryogénique de biogaz avec soutirage à un étage intermédiaire et solidification externe de dioxyde de carbone.
FR3123973B1 (fr) 2021-06-09 2023-04-28 Air Liquide Purification cryogénique de biogaz avec pré-séparation et solidification externe de dioxyde de carbone
FR3123967B1 (fr) 2021-06-09 2023-04-28 Air Liquide Procédé de séparation et de liquéfaction du méthane et du dioxyde de carbone avec solidification du dioxyde de carbone à l’extérieur de la colonne de distillation.
FR3123968B1 (fr) * 2021-06-09 2023-04-28 Air Liquide Procédé de séparation et de liquéfaction du méthane et du CO2 comprenant le soutirage de vapeur d’un étage intermédiaire de la colonne de distillation
FR3123969B1 (fr) 2021-06-09 2023-04-28 Air Liquide Procédé de séparation et de liquéfaction du méthane et du dioxyde de carbone avec pré-séparation en amont de la colonne de distillation

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4163652A (en) * 1976-03-26 1979-08-07 Snamprogetti S.P.A. Refrigerative fractionation of cracking-gases in ethylene production plants
GB2205933A (en) * 1987-06-12 1988-12-21 Costain Petrocarbon Separation of hydrocarbon mixtures
EP0467860A1 (fr) * 1990-07-06 1992-01-22 TPL S.p.A. Méthode de récupération d'éthylène et de propylène d'un gaz produit par pyrolyse d'hydrocarbures
US6560989B1 (en) * 2002-06-07 2003-05-13 Air Products And Chemicals, Inc. Separation of hydrogen-hydrocarbon gas mixtures using closed-loop gas expander refrigeration

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3444696A (en) * 1967-02-10 1969-05-20 Stone & Webster Eng Corp Demethanization employing different temperature level refrigerants
US5361589A (en) * 1994-02-04 1994-11-08 Air Products And Chemicals, Inc. Precooling for ethylene recovery in dual demethanizer fractionation systems
US20070062216A1 (en) * 2003-08-13 2007-03-22 John Mak Liquefied natural gas regasification configuration and method

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4163652A (en) * 1976-03-26 1979-08-07 Snamprogetti S.P.A. Refrigerative fractionation of cracking-gases in ethylene production plants
GB2205933A (en) * 1987-06-12 1988-12-21 Costain Petrocarbon Separation of hydrocarbon mixtures
EP0467860A1 (fr) * 1990-07-06 1992-01-22 TPL S.p.A. Méthode de récupération d'éthylène et de propylène d'un gaz produit par pyrolyse d'hydrocarbures
US6560989B1 (en) * 2002-06-07 2003-05-13 Air Products And Chemicals, Inc. Separation of hydrogen-hydrocarbon gas mixtures using closed-loop gas expander refrigeration

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2969746A1 (fr) * 2010-12-23 2012-06-29 Air Liquide Condensation d'un premier fluide a l'aide d'un deuxieme fluide
US10203155B2 (en) 2010-12-23 2019-02-12 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Method and device for condensing a first fluid rich in carbon dioxide using a second fluid

Also Published As

Publication number Publication date
ZA201004516B (en) 2011-03-30
CN101932368A (zh) 2010-12-29
MX2010007195A (es) 2010-09-30
WO2009083227A3 (fr) 2009-09-17
EP2225007A2 (fr) 2010-09-08
BRPI0821955A2 (pt) 2015-06-23
CA2710776A1 (fr) 2009-07-09
KR20100125228A (ko) 2010-11-30
EA201070803A1 (ru) 2011-02-28
DE102007063347A1 (de) 2009-07-02
JP2011508031A (ja) 2011-03-10
US20110041550A1 (en) 2011-02-24
WO2009083227A9 (fr) 2009-11-05

Similar Documents

Publication Publication Date Title
WO2009083227A2 (fr) Procédé et dispositif pour séparer des constituants à point d'ébullition bas de mélanges d'hydrocarbures
EP1818634B1 (fr) Procédé pour fournir du froid à une étape de séparation cryogénique d'une installation de production d'oléfine
EP3029019B1 (fr) Procédé de fabrication d'hydrocarbures
WO2007045364A2 (fr) Systeme de recuperation destine au traitement ulterieur d'un flux de gaz reforme d'une installation d'ethylene
WO2016128110A1 (fr) Séparation combinée de substances à haut et à bas point d'ébullition à partir de gaz naturel
DE102013013883A1 (de) Kombinierte Abtrennung von Schwer- und Leichtsiedern aus Erdgas
DE69909143T2 (de) Trennung von Kohlenstoffmonoxid aus stickstoffverschmutzten, Wasserstoff und Methan enthaltenden Gasgemischen
EP0318504B1 (fr) Procédé pour séparer d'un melange gazeux des hydrocarbures lourds
DE69814519T2 (de) Kryogenisches Verfahren mit Doppelsäure und externem Verdämpfer-Kondensator für eine Sauerstoff- und Stickstoffmischung
DE2405971C2 (de) Verfahren zum Abkühlen und/oder Verflüssigung eines Fluids
DE2713359B2 (de) Verfahren zur Gewinnung von Äthylen aus Crackgasen durch Tieftemperaturtechnik
DE69307399T2 (de) Wärmeintegration zwischen Säulen für Mehrsäulendestillationssystem
DE2155366C2 (de) Verfahren zum Trennen einer vorwiegend Stickstoff und Methan enthaltenden hochgespannten Erdgas-Beschickungsmischung
DE1268162B (de) Verfahren zum Zerlegen eines Gasgemisches
WO2017144151A1 (fr) Procédé et dispositif de décomposition cryogénique d'un gaz de synthèse
DE102012017485A1 (de) Verfahren zum Abtrennen von C2+-Kohlenwasserstoffen oder von C3+-Kohlenwasserstoffen aus einer Kohlenwasserstoff-reichen Fraktion
DE3244143A1 (de) Verfahren zur gaszerlegung
EP0228623B1 (fr) Procédé de séparation d'hydrocarbures en C5+ d'un courant gazeux
EP0642649A1 (fr) Procede de separation d'hydrocarbures a temperature d'ebullition superieure dans un melange gazeux.
EP1032798B1 (fr) Procede et installation pour la separation d'hydrocarbures c2 ou c2+
EP3029017A1 (fr) Procédé et système de fabrication d'hydrocarbures
DE102011115987B4 (de) Erdgasverflüssigung
DE3626560A1 (de) Verfahren zum abtrennen von c(pfeil abwaerts)4(pfeil abwaerts)-kohlenwasserstoffen aus einem gasgemisch
DE3626561A1 (de) Verfahren zum abtrennen von c(pfeil abwaerts)2(pfeil abwaerts)(pfeil abwaerts)+(pfeil abwaerts)- oder von c(pfeil abwaerts)3(pfeil abwaerts)(pfeil abwaerts)+(pfeil abwaerts)- kohlenwasserstoffen aus einem gasgemisch
DE3319986A1 (de) Verfahren zum abtrennen von c(pfeil abwaerts)2(pfeil abwaerts)(pfeil abwaerts)+(pfeil abwaerts)-kohlenwasserstoffen aus erdgas

Legal Events

Date Code Title Description
WWE Wipo information: entry into national phase

Ref document number: 200880125870.4

Country of ref document: CN

DPE1 Request for preliminary examination filed after expiration of 19th month from priority date (pct application filed from 20040101)
WWE Wipo information: entry into national phase

Ref document number: 2710776

Country of ref document: CA

Ref document number: 2008867264

Country of ref document: EP

WWE Wipo information: entry into national phase

Ref document number: 2010540068

Country of ref document: JP

Ref document number: 3993/CHENP/2010

Country of ref document: IN

Ref document number: MX/A/2010/007195

Country of ref document: MX

NENP Non-entry into the national phase

Ref country code: DE

ENP Entry into the national phase

Ref document number: 20107016026

Country of ref document: KR

Kind code of ref document: A

WWE Wipo information: entry into national phase

Ref document number: PI 2010003049

Country of ref document: MY

Ref document number: 201070803

Country of ref document: EA

WWE Wipo information: entry into national phase

Ref document number: 12735255

Country of ref document: US

ENP Entry into the national phase

Ref document number: PI0821955

Country of ref document: BR

Kind code of ref document: A2

Effective date: 20100629